RU89523U1 - INSTALLATION OF PROCESSING OF SOLID HYDROCARBON RAW MATERIALS - Google Patents

Abstract

1. Installation for processing solid hydrocarbon raw materials, including preparation blocks, heating blocks for raw materials, blocks for obtaining final products, characterized in that the unit includes a block of finely divided solid hydrocarbons, the unit also includes a block for preheating of molecular hydrogen and / or light hydrogen-containing media enriched with hydrogen, for example, natural or associated gas, gas and light fractions of the oil refining and petrochemicals, in particular gas and light fractions obtained during processing according to this utility model, a processing reactor-processor is included in the installation, in which hydrocarbon granules or powder of crushed raw materials are brought into direct interaction with a stream of molecular hydrogen and / or light hydrogen-containing media enriched with hydrogen for reaction with heated and / or cracked raw materials moreover, cracking of light hydrocarbons with the formation of light radicals, which are catalysts for the degradation of raw materials, occurs in the reactor-processor, light products cations are continuously withdrawn from the reaction zone and used in commercial product units for producing light commercial products, and the processing reactor-processor is combined with the heating and / or cracking unit of the raw materials in one apparatus. ! 2. The installation according to claim 1, characterized in that the installation includes a unit for cleaning light reaction products from harmful impurities, as well as cooling and condensation units for the reaction products. ! 3. Installation according to claim 1, characterized in that the device includes a device for mixing particles (granules) of solid hydrocarbon feedstocks

Description

The utility model relates to the chemical, as well as to the fuel and energy industry, and specifically to the field of processing of solid hydrocarbon materials (for example, coal, oil shale, plant products and other solid hydrocarbon media), hereinafter raw materials, and can be used in the production of hydrocarbon fuel and chemical products. In addition, the application of the utility model allows solving many environmental problems and leads to an improvement in the environmental situation. Light target products or fractions are understood as fractions for further processing and obtaining light target commercial products with a boiling point mainly up to 350-360 ° C, containing fuel, i.e. the most expensive gas, gasoline, kerosene and diesel fractions, as well as products for petrochemical and chemical industries. In the future, light target fractions or products, from which, upon final processing, light target commercial products are obtained (liquefied gas, gasoline, diesel fuel, petrochemical products and other light useful products).

A known method of processing solid hydrocarbon feedstock by the method of gasification (T.V. Bukharkina, N.G. Digurov. Chemistry of natural energy and carbon materials. Textbook. M., 1998; N.A. Kirichenko. Production of hydrogen, synthesis gas and energy gas, M., 1981). Gasification is the process of the high-temperature interaction of solid hydrocarbons with water vapor, oxygen, carbon dioxide or their mixtures in order to obtain combustible gases: hydrogen, carbon monoxide, methane. They can be used as fuel and as raw materials for the chemical industry. Almost all types of gaseous, liquid and solid fuels of hydrocarbons can be gasified. The choice of raw materials for the process is usually due to economic considerations, and sometimes the direction of further use of the resulting gas mixture. As a rule, a mixture of carbon monoxide and hydrogen for the production of chemical products (synthesis gas) is obtained by gasification (conversion) of methane and other hydrocarbons, and the generator gases for the production of synthetic liquid fuels or directly for combustion are produced from solid hydrocarbons. The processes in which mixtures of gasification products are formed are very diverse and constitute a complex system of sequentially parallel reversible and irreversible reactions.

In practice, coal is gasified with a sufficiently high content of heteroatoms, in particular, brown coal grades at temperatures of 1000-1400 ° C. It is believed that under these conditions, gasification reactions themselves are preceded by coal pyrolysis with the release of volatiles and the formation of a solid carbon-enriched residue (coke). Gasification agents then react with gaseous pyrolysis products and coke particles.

If it is necessary to obtain a gas, mainly containing hydrogen and hydrocarbons, gasification should be carried out in the low temperature region with an excess of water. This way is used if gasification is aimed at producing hydrogen. If the task is to obtain mainly carbon monoxide, then the process is carried out at higher temperatures.

The disadvantages of this method of processing solid hydrocarbon feedstocks are: high process temperature, contamination of the processed products with heteroatomic compounds, a small set of final reaction products that do not allow to obtain valuable valuable products such as motor fuels (gasoline, diesel fuel, kerosene, petrochemical products). Therefore, at present, methods for producing synthesis gas from hydrocarbons, primarily from methane, are finding wider application.

A known method of processing solid hydrocarbon feedstock by the method of hydrogenation. Hydrogenation of coal and other solid hydrocarbon feedstocks is the conversion of high molecular weight organic coal under pressure of hydrogen into liquid and gaseous products at 400-500 ° С in the presence of various solvents, donor-paste-formers, catalysts (I.V. Kaleya. Chemistry of hydrogenation processes in processing fuel. M., 1973; A.A. Krichko, V.V. Lebedev, I.L. Farberov. Non-fuel use of coal. M, 1978.). The scientific foundations of this process were developed at the beginning of the 20th century by V.N. Ipatiev, N.D. Zelinsky, F. Bergius, F. Fisher and others. In the thirties of the 20th century, industrial enterprises were built in some countries, in particular in Germany and the United Kingdom, to produce gasoline, diesel fuel, lubricants, paraffins, phenols, and other products from coal. In the forties, the production of liquid coal products exceeded 4 million tons per year. With the growth of oil production, the production of synthetic liquid fuels from coal has practically ceased, as its cost was 5-7 times higher than the cost of motor fuel derived from oil. However, in connection with the imminent depletion of oil reserves in the near future, the problem of involving solid fuels, mainly coal, in processing to produce liquid products - oil substitutes - has become again relevant.

For the hydrogenation of coal, non-oxidized brown coal is used. The content of the mineral part in them should not exceed 5-6%.

High-ash coals must first be enriched. The organic mass of coal with a carbon content of 70-85%, usually used for hydrogenation, is a self-associated multimer consisting of spatially structured blocks (oligomers). Blocks include macromolecules of carbon atoms, hydrogen and heteroatoms (oxygen, nitrogen, sulfur and others). In blocks, donor – acceptor interactions are carried out, including hydrogen bonds being formed. The breaking energy of such bonds does not exceed 30 kJ / mol (kilojoule per mole). Inside the blocks, the macromolecules are linked by methylene, as well as oxygen, nitrogen, and sulfur-containing bridges. The energy of breaking these bonds is 10-15 times greater than the energy of breaking blocks. When coal is hydrogenated, the separation of the blocks occurs first. Subsequent destruction of the blocks requires elevated temperature. To obtain liquid products from coal, it is necessary, along with destruction, to saturate the resulting low molecular weight unsaturated compounds with hydrogen.

To increase the degree of conversion of the organic mass of coal into liquid products, a catalyst is applied to coal (from salt solutions, in the form of a powder, emulsion or suspension) in an amount of 1-5% by weight of coal. The more active the catalyst, the lower the pressure the coal can be hydrogenated. Molybdenum and vanadium have the maximum catalytic activity, when using which hydrogenation can be carried out at a relatively low pressure of 10-14 MPa. However, their use is limited due to the difficulty of regeneration from the mixture with the remainder of the unconverted coal.

In the process of coal hydrogenation, a donor-pastifier is necessarily used, in a mixture with which (50-60% of the pastor) coal is processed. High boiling fractions of oil refining, which are oil refining residues or oil residues, are used as a donor-paste former.

The disadvantage of the process of processing solid hydrocarbons by hydrogenation is the high cost of the resulting target products. In addition, high-boiling fractions forming a donor-paste former, which are heavy oil residues, will very quickly lead to coking of the active surface of any catalyst. Due to the high content of metals, asphaltenes in oil residues, along with sulfur, nitrogen compounds and other harmful impurities and components, catalysts are rapidly deactivated, pores are closed, the surface of the catalyst is covered with tar and coke deposits. All this significantly reduces the selectivity and efficiency of the classical catalytic process. The need for continuous manufacture and renewal of catalysts, their rapid change and disposal requires additional capital and operating costs and increases the cost of the processing process and the resulting products.

The closest analogue (prototype) is the process of hydrogenation of solid hydrocarbon feedstocks.

The purpose of the utility model is to reduce the cost of the process (operating and capital costs) by reducing the process temperature and / or reducing or preventing coking and poisoning of the process catalyst with raw materials and its impurities.

The technical result, the proposed utility model is aimed at, and the goal is achieved by organizing a process scheme in which the feedstock and the catalyst do not contact, so that the catalyst is practically not poisoned by harmful impurities and does not coke, which leads to an increase in the durability of the catalyst and the absence of the need for processes regeneration. The technical result is also achieved due to the fact that the destruction of the raw material is carried out when it is heated in the presence of active atomic hydrogen and / or light hydrocarbon radicals, which are very active in chemical reactions, therefore, serve as catalysts in the process of destruction of raw materials, which leads to a decrease process temperature. The process of destruction of solid hydrocarbons is intensified and the temperature of the process decreases. To achieve a high processing depth, the raw material or its part is subjected to the processing process according to this utility model repeatedly, possibly repeatedly.

This object is achieved by the fact that gaseous molecular hydrogen and / or light hydrogen-containing fractions enriched with hydrogen, for example, associated or natural gas, or process gas, methane, propane-butane mixtures, pentane fractions, xylene, toluene, light, are in direct contact with the heated catalyst shoulder straps of gasoline fractions, including process fractions, etc., used to produce active atomic hydrogen and / or light radicals, which then react with heated to a certain temperature yrem. Molecular hydrogen and / or light hydrogen-containing products do not contain asphaltenes, carbenes, gummy and coke-like substances, etc., as well as harmful impurities, and their interaction with the catalyst does not lead to its coking and poisoning. Heavy raw materials do not come into direct contact with the catalyst, poisoning and coking do not occur, there is no need for catalyst regeneration, the process is simplified and becomes more reliable, the cost of the process and equipment is significantly reduced, i.e. there is a decrease in capital and operating costs, the processing depth can be increased to 100%.

Solid (for example, coal, shale, vegetable products and other solid hydrocarbons) feedstock after the preparation unit (drying, enrichment of the organic part, purification from mechanical and other impurities, etc.) are sent to the fine grinding unit, in which the raw materials are converted powder to increase the reaction surface of the raw material. The granule size is predominantly up to 0.01 millimeters, although granules of large sizes can be used, but the reaction will go slower and the amount of unreacted raw materials, which must be returned for recycling, will increase.

Then, the hydrocarbon powder (granules) is sent to the processing reactor-processor, combined with the heating and / or cracking unit of the feedstock. In a reactor reactor, the feed is heated or heated and subjected to non-catalytic cracking, for example thermal cracking. Cracking of solid hydrocarbon feeds means (based on the above-described structure of solid hydrocarbons) the separation and destruction of blocks and macromolecules. You can also use any other types of cracking - with the help of an electric arc, electromagnetic or radioactive radiation, etc., but currently, of all the options for non-catalytic cracking in industry, only thermal is used.

Molecular hydrogen and / or light hydrogen-containing media enriched with hydrogen, for example, associated gas, natural gas, including gas and part of the light fractions of hydrocarbon processing, for example, oil refining and petrochemicals, if necessary (especially if the hydrogen-containing raw material is a liquid and it is necessary transfer to the gas-vapor phase) are heated in the block for preheating hydrogen and / or hydrogen-containing media separately from the raw material, they are sent at a pressure higher than the pressure in the block for heating and / or cracking to obtain atomic hydrogen and / or light radicals to a reactor with a catalyst heated to the required temperature (unit for producing atomic hydrogen and / or light radicals), after which active hydrogen and / or light radicals are sent to the processing reactor-processor, combined with the heating unit and / or cracking the feed into a heating and / or cracking zone for carrying out the reaction. A reactor with a catalyst is also a collector for uniform distribution of atomic hydrogen and / or light radicals over the cross section and volume of the reactor processor.

Under the influence of high temperatures, the destruction and splitting of blocks and macromolecules of the raw material into unsaturated radicals occurs. In addition, atomic hydrogen and / or light radicals are very active in carrying out chemical reactions, therefore, they serve as catalysts in the process of destruction of raw materials, which leads to a decrease in the temperature of the process. In the reactor reactor, direct interaction of active atomic hydrogen and / or light radicals with unsaturated radicals resulting from the destruction of the macromolecules of raw materials is carried out. As a result of the reaction, the open bonds of the radicals of degradation of the feed are saturated with atomic hydrogen and / or light radicals and saturated light hydrocarbons are formed, which are a good raw material for the preparation of motor fuel and petrochemical products.

The raw materials and the catalyst do not contact, as a result of which the catalyst is practically not poisoned by harmful impurities and does not coke, which leads to an increase in the durability of the catalyst and the absence of the need for regeneration processes and, ultimately, to reduce the cost of the process. In addition, the process temperature decreases, i.e. degradation temperature of raw materials, as the process is intensified due to the chemical activity of atomic hydrogen and / or light radicals, which are also expendable catalysts of the process.

The reaction products after the reactor processor are sent to the purification unit from harmful impurities, if necessary, they are cooled and condensed and sent to the units for producing light commercial products, mainly with a boiling point up to 350-360 ° С (liquefied gas, gasoline, diesel fuel, petrochemical products and other light useful products) at the place of processing of raw materials according to this utility model or transported to a remote place of processing to obtain light commercial products.

Thus, part of the solid hydrocarbon feedstock is processed into the target products - light hydrocarbon fractions, the process slows down, therefore, with the industrial implementation of the proposed utility model, it is necessary to continuously remove unreacted residual feedstock from the reactor processor and replace it with fresh one. Therefore, the scheme includes blocks for cleaning and sorting partially reacted solid hydrocarbon feeds, which are removed from the reaction zone, refined and sorted unreacted feeds are returned to the reaction zone, and fresh solid hydrocarbon feeds after the fine grinding block are also introduced there. During repeated processing, solid hydrocarbon raw materials can be completely, almost 100%, processed into light target hydrocarbon fractions or products.

Gives a positive effect and a variant of the process of periodic action. Solid hydrocarbon feeds are crushed, loaded into a processing reactor-processor, combined with a heating and / or cracking unit of the feed, in which reactive atomic hydrogen and / or light radicals are reacted with unsaturated radicals of the feed. After the reaction, the reactor processor is completely cleaned and loaded with fresh raw materials.

In order to further reduce costs, unreacted hydrogen and / or light hydrogen-containing media enriched with hydrogen are, if necessary, purified from harmful impurities and returned to the beginning of the process for recycling.

Granules of crushed solid hydrocarbon materials have a rather active surface, which can lead to adhesion of the granules and a decrease in the active reaction surface and the efficiency and intensity of the process. To prevent sticking of particles (granules) of solid hydrocarbon feedstocks, the reactor-processor of solid hydrocarbon feedstocks is combined with a mixing device. This can be a mechanical mixer, or a device that allows continuous vibration of the reactor processor, or the mixing is organized due to the pressure of the gases supplied to the reactor processor, i.e. the process is in a fluidized bed of suspended particles. Other mixing options may be used.

Atomic hydrogen is much more active than molecular hydrogen. So, atomic hydrogen, under ordinary conditions, combines with sulfur, phosphorus, arsenic, etc., reduces the oxides of many metals, displaces some metals (copper, lead, etc.) from their salts and enters into other chemical reactions to which ordinary molecular hydrogen is not capable of the same conditions. The rate of reactions of formation of atomic hydrogen from molecular and light hydrogen-containing media increases with the use of catalysts (platinum group metals, transition or heavy metal oxides, aluminosilicate, zeolite-containing and other types of catalysts), methods of excitation by means of wave action with a wide spectrum of frequencies of various nature and intensity (light , electric discharge, electric arc, etc.), as well as using chemical reactions. In an atomic form, hydrogen reacts with almost any elements and molecules, except for noble gases (B. Nekrasov, Fundamentals of General Chemistry. M., 1973). Light radicals have the same high activity. Therefore, they react with hydrocarbon molecules, and not just with radicals of raw materials. In addition, atomic hydrogen and / or light radicals are very active in carrying out chemical reactions, therefore, they serve as catalysts in the process of destruction of raw materials, which leads to a decrease in the temperature of the process. Those. the temperature of the hydrocarbon processing process may be lower than the cracking temperature, which leads to cheaper equipment and process costs.

Obtaining atomic hydrogen and / or light radicals using the methods of wave excitation and chemical reactions under industrial conditions of the oil refining complex is not yet the most effective way, although with the further development and optimization of such processes it has a good prospect.

The most real results in industrial conditions can be achieved using catalysts. For this, gaseous molecular hydrogen, hydrogen-containing media and / or a reactor with a catalyst are heated to a temperature of 300-500 ° C, and sometimes higher (although more effective catalysts can be found over time that will allow the formation of hydrogen and / or light radicals at lower temperatures, for example, at 20-100 ° C and below). In the interaction of hydrogen and / or hydrogen-containing media with molybdenum, cobalt, zinc, vanadium, nickel, aluminosilicate, zeolite-containing and other catalysts, for example based on aluminum oxide, or other types of catalysts, atomic hydrogen and / or light radicals are formed, which effectively interacts with hydrocarbon molecules and saturate open bonds of radicals obtained as a result of the cracking reaction of the hydrocarbon feedstock, resulting in the formation of saturated light target fractions of higher quality.

When implementing the proposed utility model, the feedstock is purified from sulfur and other impurities. The carbon-heteroatom bond energies (carbon - sulfur, carbon - nitrogen, etc.) are lower than the carbon - carbon and carbon - hydrogen bonds (T.V. Bukharkina, N.G. Digurov. Chemistry of natural energy carriers and carbon materials. M. , 1998). Therefore, for example, sulfur atoms, the purification of the feedstock from which is problematic, are more likely to disconnect from the hydrocarbon molecule during cracking, and when this utility model is implemented, they form hydrogen sulfide. Hydrogen sulfide is easily released in a gaseous form and disposed of to produce atomic sulfur or other sulfur-containing commercial products.

The task of processing solid hydrocarbons is also solved by the fact that a mixture of crushed solid hydrocarbon feedstocks and catalyst granules is placed in the reactor processor. Additionally, a mixer for mixing particles of raw materials and catalyst is included in the processing scheme (block for preparing a mixture of raw materials and catalyst). When implementing this option, molecular hydrogen and / or light hydrogen-containing media enriched with hydrogen, for example, associated gas, natural gas, including gas and part of the light fractions of hydrocarbon feed processing, such as oil refining and petrochemicals, if necessary (especially if the hydrogen-containing feed is the liquid and it must be transferred to the vapor-gas phase) are heated in the unit for preheating hydrogen and / or hydrogen-containing media and fed to the processing reactor-processor, combined with the heating unit and / or cracking but raw materials. For a uniform distribution of hydrogen-containing media over the cross section and volume of the reactor processor, they are fed using a collector. In this embodiment, a reactor with a catalyst (unit for producing atomic hydrogen and / or light radicals) is not used. The cracking of both raw materials and molecular hydrogen and / or light hydrogen-containing media enriched with hydrogen is carried out in the reactor processor under the influence of temperature and the process catalyst. In the reactor reactor, the resulting active atomic hydrogen and / or light radicals interact directly with unsaturated radicals resulting from the degradation of the macromolecules of the feedstock. As a result of the reaction, the open bonds of the radicals of degradation of the feed are saturated with atomic hydrogen and / or light radicals and saturated light hydrocarbons are formed, which are a good raw material for the preparation of motor fuel and petrochemical products.

The reaction products after the reactor processor are sent to the purification unit from harmful impurities, if necessary, they are cooled and condensed and sent to the units for producing light commercial products, mainly with a boiling point up to 350-360 ° С (liquefied gas, gasoline, diesel fuel, petrochemical products and other light useful products) at the place of processing of raw materials according to this utility model or transported to a remote place of processing to obtain light commercial products.

The scheme also includes blocks for the purification and sorting of partially reacted solid hydrocarbon feeds, which are removed from the reaction zone together with the catalyst, refined and sorted unreacted feeds and the catalyst are returned to the reaction zone, and fresh solid hydrocarbon feeds after the fine grinding block are also introduced there. During repeated processing, solid hydrocarbon raw materials can be completely, almost 100%, processed into light target hydrocarbon fractions or products.

In order to further reduce costs, unreacted hydrogen and / or light hydrogen-containing media enriched with hydrogen are, if necessary, purified from harmful impurities and returned to the beginning of the process for recycling.

To prevent sticking of particles (granules) of solid hydrocarbon feedstocks, the reactor-processor of solid hydrocarbon feedstocks is combined with a mixing device. This can be a mechanical mixer, or a device that allows continuous vibration of the reactor processor, or the mixing is organized due to the pressure of the gases supplied to the reactor processor, i.e. the process is in a fluidized bed of suspended particles. Other mixing options may be used.

In this embodiment, the donor-paste former is not used, in a mixture with which (50-60% of the paste former) coal is processed using the prototype (high-boiling fractions of oil refining, which are oil refining residues or oil residues and contain resins, asphaltenes, are used as a donor pastor) and many harmful impurities). Therefore, the process catalyst is much less coked and poisoned by impurities of the donor-paste former, which leads to a decrease in capital and operating costs, i.e. to reduce the cost of the process. In addition, the process temperature decreases, i.e. degradation temperature of raw materials, as the process proceeds in the presence of a catalyst and is intensified due to the chemical activity of atomic hydrogen and / or light radicals, which are also catalysts of the process.

The problem is also solved by the fact that the catalysts are not used, and the destruction of blocks and macromolecules of raw materials and light hydrocarbons occurs only under the influence of high temperature (thermal cracking). When implementing this option, molecular hydrogen and / or light hydrogen-containing media enriched with hydrogen, for example, associated gas, natural gas, including gas and part of the light fractions of hydrocarbon feed processing, such as oil refining and petrochemicals, if necessary (especially if the hydrogen-containing feed is the liquid and it must be transferred to the vapor-gas phase) are heated in the unit for preheating hydrogen and / or hydrogen-containing media and fed to the processing reactor-processor, combined with the heating unit and / or cracking but raw materials. For a uniform distribution of hydrogen-containing media over the cross section and volume of the reactor processor, they are fed using a collector. The cracking of both raw materials and molecular hydrogen and / or light hydrogen-containing media enriched with hydrogen is carried out in the reactor processor under the influence of the process temperature. In the reactor reactor, the direct interaction of the generated active atomic hydrogen and / or light radicals with unsaturated radicals resulting from the destruction of the macromolecules of the raw material is carried out. As a result of the reaction, the open bonds of the radicals of degradation of the feed are saturated with atomic hydrogen and / or light radicals and saturated light hydrocarbons are formed, which are a good raw material for the preparation of motor fuel and petrochemical products.

The reaction products after the reactor processor are sent to the purification unit from harmful impurities, if necessary, they are cooled and condensed and sent to the units for producing light commercial products, mainly with a boiling point up to 350-360 ° С (liquefied gas, gasoline, diesel fuel, petrochemical products and other light useful products) at the place of processing of raw materials according to this utility model or transported to a remote place of processing to obtain light commercial products.

The scheme also includes blocks for the purification and sorting of partially reacted solid hydrocarbon raw materials, which are removed from the reaction zone, the purified and sorted unreacted raw materials are returned to the reaction zone, and fresh solid hydrocarbon raw materials are also introduced there after the block of fine grinding. During repeated processing, solid hydrocarbon raw materials can be completely, almost 100%, processed into light target hydrocarbon fractions or products.

In order to further reduce costs, unreacted hydrogen and / or light hydrogen-containing media enriched with hydrogen are, if necessary, purified from harmful impurities and returned to the beginning of the process for recycling.

To prevent sticking of particles (granules) of solid hydrocarbon feedstocks, the reactor-processor of solid hydrocarbon feedstocks is combined with a mixing device. This can be a mechanical mixer, or a device that allows continuous vibration of the reactor processor, or the mixing is organized due to the pressure of the gases supplied to the reactor processor, i.e. the process is in a fluidized bed of suspended particles. Other mixing options may be used.

In this embodiment, the catalyst does not coke and is not poisoned by harmful impurities, which leads to a decrease in the cost of the process, and the process temperature is much higher than in previous versions. But the temperature of the process is much lower than with conventional thermal destruction of solid hydrocarbons, because the process is intensified due to the chemical activity of atomic hydrogen and / or light radicals, which are catalysts of the process.

In figures 1-3 presents enlarged schematic diagrams of the processing of solid hydrocarbon feedstocks.

Figure 1-3 indicated: 1 - block finely divided raw materials; 2 - processing reactor-processor, combined with a block of heating and / or cracking of raw materials; 3 - block heating of molecular hydrogen and / or light hydrogen-containing media enriched with hydrogen; 4 - block purification of light reaction products from harmful impurities; 5 - blocks for cleaning and sorting partially reacted solid hydrocarbon feedstocks or feedstocks and catalysts; 6 - mixer for mixing particles of raw materials and catalyst (unit for preparing a mixture of raw materials and catalyst); 7 - a reactor or reactor pack with a catalyst heated to the required temperature to produce active atomic hydrogen and / or light radicals from molecular hydrogen and / or light hydrogen-containing media (unit for producing atomic hydrogen and / or light radicals).

Block preparation of raw materials for simplicity in the figures not shown. Also, for simplicity, the blocks for obtaining marketable products and infrastructure elements — commodity parks, treatment facilities, etc., are not presented.

If you use only thermal processes, it is advisable to use the processing scheme presented in figure 1. Prepared raw materials are fed into the block of fine grinding of raw materials (figure 1, position 1), then to the processing reactor-processor, combined with the block of heating and / or cracking of raw materials (figure 1, position 2). Hydrogen or light hydrogen-containing media are fed to the heating unit (Fig. 1, position 3), then to the reactor processor (Fig. 1, position 2), where the active atomic hydrogen and / or light radicals formed under the influence of temperature are directly interacted with unsaturated radicals resulting from the degradation of macromolecules of raw materials under the influence of high temperature. As a result of the reaction, the open bonds of the radicals of degradation of the feed are saturated with atomic hydrogen and / or light radicals and saturated light hydrocarbons are formed, which are a good raw material for the preparation of motor fuel and petrochemical products. After the reactor processor, the reacted raw materials are sent to the purification unit (Fig. 1, position 4) and then (if necessary, after cooling and condensation) to obtain marketable products. The partially reacted solid hydrocarbon feed, which is removed from the reaction zone, is sent to the purification and sorting units (Fig. 1, position 5), the purified and sorted unreacted feed is returned to the reaction zone (if necessary after grinding), and fresh solid hydrocarbon feed is also introduced there. raw materials after a block of fine grinding. Unreacted hydrogen and / or light hydrogen-containing media enriched with hydrogen are removed from the reactor processor, if necessary, cleaned of harmful impurities and returned to the beginning of the process for reprocessing.

If you use a scheme with mixing granules of raw materials and catalyst, it is advisable to use the processing scheme presented in figure 2. Prepared raw materials are fed to the block of finely divided raw materials (Fig. 2, position 1), then to the mixer (Fig. 2, position 6) to mix the particles of raw materials and catalyst (the unit for preparing the mixture of raw materials and catalyst), the catalyst is also fed there. Then the mixture of granules of raw materials and catalyst is fed into the processing reactor-processor, combined with the block of heating and / or cracking of raw materials (figure 2, position 2). Hydrogen or light hydrogen-containing media are fed to the heating unit (Fig. 2, position 3), then to the reactor processor (Fig. 2, position 2), where the active atomic hydrogen and / or light radicals formed under the influence of temperature and catalyst are directly interacted with with unsaturated radicals resulting from the destruction of the macromolecules of the raw material under the influence of temperature and catalyst. As a result of the reaction, the open bonds of the radicals of degradation of the feed are saturated with atomic hydrogen and / or light radicals and saturated light hydrocarbons are formed, which are a good raw material for the preparation of motor fuel and petrochemical products. After the reactor-processor, the reacted raw materials are sent to the purification unit (Fig. 2, position 4) and then (if necessary, after cooling and condensation) to obtain marketable products. The partially reacted solid hydrocarbon feed, which is removed from the reaction zone, is sent to the purification and sorting units (Fig. 2, position 5), the purified and sorted unreacted feed, and the catalyst are returned to the reaction zone (if necessary after grinding), and fresh solid hydrocarbon feed after a block of fine grinding. Unreacted hydrogen and / or light hydrogen-containing media enriched with hydrogen are removed from the reactor processor, if necessary, cleaned of harmful impurities and returned to the beginning of the process for reprocessing.

If you use a scheme in which the catalyst is not in contact with the feed, it is advisable to use the processing scheme shown in figure 3. Prepared raw materials are fed into the block of fine grinding of raw materials (figure 3, position 1), then to the processing reactor-processor, combined with the block of heating and / or cracking of raw materials (figure 3, position 2). Hydrogen or light hydrogen-containing media are fed into a heating unit (Fig. 3, position 3), then a reactor or reactor package (Fig. 3, position 7) with a catalyst heated to the required temperature to produce active atomic hydrogen and / or light radicals from molecular hydrogen and / or light hydrogen-containing media (unit for producing atomic hydrogen and / or light radicals), then to the reactor processor (Fig. 3, position 2), where direct interaction of active atomic hydrogen and / or light radicals with unsaturated rad icals formed as a result of destruction of raw macromolecules. As a result of the reaction, the open bonds of the radicals of degradation of the feed are saturated with atomic hydrogen and / or light radicals and saturated light hydrocarbons are formed, which are a good raw material for the preparation of motor fuel and petrochemical products. After the reactor-processor, the reacted raw materials are sent to block cleaners (Fig. 3, position 4) and then (if necessary, after cooling and condensation) to obtain marketable products. The partially reacted solid hydrocarbon feed, which is removed from the reaction zone, is sent to the purification and sorting units (Fig. 3, position 5), the purified and sorted unreacted feed is returned to the reaction zone (if necessary after grinding), and fresh solid hydrocarbon feed is also introduced there. raw materials after a block of fine grinding. Unreacted hydrogen and / or light hydrogen-containing media enriched with hydrogen are removed from the reactor processor, if necessary, cleaned of harmful impurities and returned to the beginning of the process for reprocessing.

Example 1

In laboratory conditions, experiments were carried out using a small experimental reactor processor. A schematic diagram of a reactor-processor is shown in figure 4, which indicates (in accordance with the uniform designations in figures 1-3): 2 - processing reactor-processor, combined with a block of heating and / or cracking of raw materials; 7 - a reactor or reactor pack with a catalyst heated to the required temperature to produce active atomic hydrogen and / or light radicals from molecular hydrogen and / or light hydrogen-containing media (unit for producing atomic hydrogen and / or light radicals). The initial crushed solid hydrocarbon feed is placed in a reactor processor, which is heated in a muffle furnace (figure 4, position 2). The volume of the reactor processor is 400 cubic centimeters. The reactor processor is equipped with thermocouples for measuring temperature and a sensor for measuring pressure. In the lower part of its body there is an integrated reactor with a catalyst (unit for producing atomic hydrogen and / or light radicals). The heating of the catalyst in a reactor with a catalyst, as well as hydrogen and / or light hydrogen-containing media, is also carried out in a muffle furnace in the supply pipes and the reactor itself with a catalyst. In these experiments, the temperature of the raw material was mainly 400-600 ° C and higher, the pressure in the reactor processor to 1 MPa. In the presence of chemically active atomic hydrogen and / or active light radicals, the destruction of solid hydrocarbon materials occurs more intensively and at lower temperatures. Propane - butane mixture from a cylinder is fed (at a higher pressure than the pressure in the reactor-processor) into a reactor with a catalyst (Fig. 4, position 7) with a nickel, molybdenum or platinum catalyst (in the form of granules with a diameter of up to 1 millimeter) embedded in it . The propane-butane mixture and the reactor with the catalyst are heated in this embodiment to the required temperature due to the heat of the heated feedstock. The reactor with the catalyst is arranged in the form of a flat cylinder into which the catalyst is placed, mounted horizontally in cross section at the bottom of the reactor processor, with a hydrogen supply pipe for the distribution of hydrogen-containing media over the cross section of the reactor with the catalyst and openings distributed throughout the upper plane of the reactor 0.1 mm in diameter for the distribution of the resulting atomic hydrogen and / or light radicals over the cross section of the reactor processor. The design of the reactor with the catalyst can be double-sided, spherical, etc., this is not of fundamental importance. Atomic hydrogen and / or light radicals formed in the reactor with the catalyst are distributed over the entire cross section of the reactor processor and enter directly into the destruction zone of the feedstock, where the saturation reaction of open bonds of the feedstock radicals takes place. Light reaction fractions are discharged through the upper pipe with a valve from the reactor processor, cooled and analyzed. Shale crushed to a size of less than 0.01 millimeters with an organic content of about 90% was used as raw material. The yield of light target gas and light fractions with a boiling point of up to 350-360 ° C amounted to approximately 81% of the mass of solid hydrocarbon feed (shale) loaded into the reactor processor. Hydrogen sulfide was present in the reaction products, but it was not possible to determine its mass fraction. With repeated processing (with the return of unreacted raw materials to reprocessing), the yield of the target fractions will increase to almost 100%. When using hydrogen from a cylinder instead of a propane-butane mixture, almost identical results were obtained. Other light hydrogen-rich products or fractions can also be used. This approach is not a prototype of the industrial process, but makes it easy to demonstrate the specific implementation of the proposed utility model.

Example 2

In this example, the same reactor-processor was used, but a mixture of raw materials and a catalyst in the ratio of 10: 1 was loaded into it (the catalyst is the same as in example 1). The catalyst was not loaded into the reactor with the catalyst; it was used as a collector for supplying light hydrogen-containing media enriched in hydrogen to the reactor processor. A schematic diagram of a reactor-processor is shown in Fig. 5, which indicates (in accordance with the uniform notation in Figs. 1-4): 2 - a processing reactor-processor combined with a heating and / or cracking unit for raw materials; 8 - collector for the distribution of molecular hydrogen and / or light hydrogen-containing media over the cross section of the reactor processor. A mixture of crushed solid hydrocarbon feed and catalyst is placed in a reactor processor, which is heated in a muffle furnace (figure 5, position 2). Heating of light hydrogen-containing media is also carried out in a muffle furnace in the supply piping and manifold. In these experiments, the temperature of the feed was also mainly 400-600 ° C and above, the pressure in the reactor processor to 1 MPa. In the presence of a catalyst and chemically active atomic hydrogen and / or active light radicals, which are formed in the reactor processor under the influence of temperature and catalyst, the destruction of solid hydrocarbon materials occurs more intensively and at lower temperatures. The propane-butane mixture from the cylinder is fed (at a higher pressure than the pressure in the reactor processor) to the collector (figure 5, position 8). The propane-butane mixture is heated in this embodiment to the required temperature due to the heat of the heated feedstock. The collector is arranged in the form of a flat cylinder mounted horizontally in cross section at the bottom of the reactor processor, with a hydrogen supply pipe for distributing hydrogen-containing media over the cross section of the reactor processor and holes 0.1 mm in diameter distributed over the entire upper plane of the collector. Atomic hydrogen and / or light radicals formed in the reactor-processor are distributed over the entire cross section of the reactor-processor and are located directly in the destruction zone of the feedstock, where the saturation reaction of open bonds of the radicals of the feedstock takes place. Light reaction fractions are discharged through the upper pipe with a valve from the reactor processor, cooled and analyzed. Shale crushed to a size of less than 0.01 millimeters with an organic content of about 90% was used as raw material. The yield of light target gas and light fractions with a boiling point of up to 350-360 ° C amounted to approximately 78% of the mass of solid hydrocarbon feed (shale) loaded into the reactor processor. Hydrogen sulfide was present in the reaction products, but it was not possible to determine its mass fraction. With repeated processing (with the return of unreacted raw materials to reprocessing), the yield of the target fractions will increase to almost 100%. When using hydrogen from a cylinder instead of a propane-butane mixture, almost identical results were obtained. Other light hydrogen-rich products or fractions can also be used. This approach is not a prototype of the industrial process, but makes it easy to demonstrate the specific implementation of the proposed utility model.

Example 3

In this example, the same reactor processor was used. The catalyst was not loaded into the reactor with the catalyst; it was used as a collector for supplying light hydrogen-containing media enriched in hydrogen to the reactor processor. A schematic diagram of a reactor-processor is shown in Fig. 5, which indicates (in accordance with the uniform notation in Figs. 1-4): 2 - a processing reactor-processor combined with a heating and / or cracking unit for raw materials; 8 - collector for the distribution of molecular hydrogen and / or light hydrogen-containing media over the cross section of the reactor processor. The crushed solid hydrocarbon feed is placed in a reactor processor, which is heated in a muffle furnace (figure 5, position 2). Heating of light hydrogen-containing media is also carried out in a muffle furnace in the supply piping and manifold. In these experiments, the temperature of the raw material was mainly 700-900 ° C and higher, the pressure in the reactor processor to 1 MPa. In the presence of reactive atomic hydrogen and / or active light radicals, which are formed in the reactor processor under the influence of temperature, the destruction of solid hydrocarbon materials occurs more intensively and at lower temperatures than only under the influence of temperature. Propane - butane mixture from the cylinder is fed (at a higher pressure than the pressure in the reactor processor) into the collector (figure 5, position 8). Propane - butane mixture is heated in this embodiment to the required temperature due to the heat of the heated raw materials. The collector is arranged in the form of a flat cylinder mounted horizontally in cross section at the bottom of the reactor processor, with a hydrogen supply pipe for distributing hydrogen-containing media over the cross section of the reactor processor and holes 0.1 mm in diameter distributed over the entire upper plane of the collector. Atomic hydrogen and / or light radicals formed in the reactor-processor are distributed over the entire cross section of the reactor-processor and are located directly in the destruction zone of the feedstock, where the saturation reaction of open bonds of the radicals of the feedstock takes place. Light reaction fractions are discharged through the upper pipe with a valve from the reactor processor, cooled and analyzed. Shale, crushed to sizes less than 0.01 mm, with an organic content of about 90% was also used as raw material. The yield of light target gas and light fractions with a boiling point of up to 350-360 ° C was approximately 54% of the mass of solid hydrocarbon feed (shale) loaded into the reactor processor. Hydrogen sulfide was present in the reaction products, but it was not possible to determine its mass fraction. With repeated processing (with the return of unreacted raw materials to reprocessing), the yield of the target fractions will increase to almost 100%. When using hydrogen from a cylinder instead of a propane-butane mixture, almost identical results were obtained. Other light hydrogen-rich products or fractions can also be used. This approach is not a prototype of the industrial process, but makes it easy to demonstrate the specific implementation of the proposed utility model.

In all the experiments, the reactor-processor was connected to a device that vibrates the reactor-processor to prevent adhesion of granules of crushed raw materials.

Thus, the technical result of applying the utility model is to reduce the cost of the process (operating and capital costs) by reducing the process temperature and / or reducing or preventing coking and poisoning of the process catalyst with raw materials and its impurities due to the fact that the destruction of the raw materials is carried out when it is heated in the presence of active atomic hydrogen and / or light hydrocarbon radicals. The process of destruction of solid hydrocarbons is intensified and the temperature of the process decreases. In addition, the process is organized so that the feed and the catalyst do not contact, therefore, there is a reduction or prevention of coking and poisoning of the catalyst, which also leads to a decrease in the cost of the process.

Almost 100% of the processing depth (calculated by the yield of light target fractions and products) can be achieved by this utility model due to the reprocessing of raw materials.

The proposed installation is easy to operate and does not require large capital and operating costs.

Claims (20)

1. Installation for processing solid hydrocarbon raw materials, including preparation blocks, heating blocks for raw materials, blocks for obtaining final products, characterized in that the unit includes a block of finely divided solid hydrocarbons, the unit also includes a block for preheating of molecular hydrogen and / or light hydrogen-containing media enriched with hydrogen, for example, natural or associated gas, gas and light fractions of the oil refining and petrochemicals, in particular gas and light fractions obtained during processing according to this utility model, a processing reactor-processor is included in the installation, in which hydrocarbon granules or powder of crushed raw materials are brought into direct interaction with a stream of molecular hydrogen and / or light hydrogen-containing media enriched with hydrogen for reaction with heated and / or cracked raw materials moreover, cracking of light hydrocarbons with the formation of light radicals, which are catalysts for the degradation of raw materials, occurs in the reactor-processor, light products cations are continuously withdrawn from the reaction zone and used in commercial product units for producing light commercial products, and the processing reactor-processor is combined with the heating and / or cracking unit of the raw materials in one apparatus. 2. The installation according to claim 1, characterized in that the installation includes a unit for cleaning light reaction products from harmful impurities, as well as cooling and condensation units for the reaction products. 3. The installation according to claim 1, characterized in that the device includes a device for mixing particles (granules) of solid hydrocarbon raw materials to prevent them from sticking together, and the reactor-processor of solid hydrocarbon raw materials is combined with a mixing device. 4. The installation according to claim 1, characterized in that the installation includes cleaning and sorting units for partially reacted solid hydrocarbon feed, which is removed from the reaction zone, to return the purified and sorted unreacted feed to the fine grinding unit or to the reaction zone to the reactor processor into which fresh solid hydrocarbon feed is introduced after the block of fine grinding. 5. Installation according to claim 1, characterized in that the installation includes a unit for purification from harmful impurities of unreacted hydrogen and / or light hydrogen-containing media enriched with hydrogen, to return to the beginning of the process for reprocessing. 6. Installation according to claim 1, characterized in that the installation includes a collector for distributing hydrogen and / or hydrogen-containing media over the cross section and volume of the reactor processor, the collector being combined with the reactor processor in one apparatus. 7. Installation according to claim 1, characterized in that the unit for heating hydrogen and / or hydrogen-containing media is combined in one apparatus with a reactor processor, and the heating of hydrogen and / or hydrogen-containing media is carried out due to the heat of the heated feedstock. 8. Installation for processing solid hydrocarbon raw materials, including preparation blocks, blocks for heating raw materials, blocks for producing final products, characterized in that the unit includes a block of finely divided grinding of solid hydrocarbon raw materials, a mixer for mixing particles of raw materials and catalyst is included (block for preparing a mixture of raw materials and catalyst ), the heating unit for the mixture of raw materials and catalyst is included, the unit also includes a preliminary heating unit for molecular hydrogen and / or light hydrogen-containing media, enriched with hydrogen, for example, natural or associated gas, gas and light fractions of oil refining and petrochemicals, in particular gas and light fractions obtained in the process of processing according to this utility model, a processing reactor-processor is included in the installation, in which a mixture of hydrocarbon granules or pulverized powder raw materials and catalysts are brought into direct interaction with the flow of molecular hydrogen and / or light hydrogen-containing media enriched with hydrogen for reaction with heated and / or cracked raw materials, etc. than cracking of light hydrocarbons with the formation of light radicals, which are catalysts for the destruction of raw materials, takes place in the reactor-processor, light reaction products are continuously removed from the reaction zone and used in commercial product units to produce light commercial products, and the processing reactor-processor is combined with block heating and / or cracking of raw materials in one device. 9. The installation according to claim 8, characterized in that the installation includes a unit for cleaning light reaction products from harmful impurities, as well as cooling and condensation units for the reaction products. 10. Installation according to claim 8, characterized in that the installation includes a device for mixing particles (granules) of solid hydrocarbon feedstock and a catalyst to prevent them from sticking together, and a reactor-processor of solid hydrocarbon feedstock is combined with a mixing device. 11. Installation according to claim 8, characterized in that the installation includes cleaning and sorting units for partially reacted solid hydrocarbon feeds, which are discharged in a mixture with a catalyst from the reaction zone, to return purified and sorted unreacted feeds and catalysts to the fine grinding unit or to the reaction zone into the reactor processor, into which a fresh mixture of solid hydrocarbon feedstock is introduced after the block of finely divided grinding of the feedstock and catalyst. 12. Installation according to claim 8, characterized in that the installation includes a unit for cleaning harmful impurities from unreacted hydrogen and / or light hydrogen-containing media enriched with hydrogen to return to the beginning of the process for reprocessing. 13. Installation according to claim 8, characterized in that the installation includes a collector for distributing hydrogen and / or hydrogen-containing media over the cross section and volume of the reactor processor, the collector being combined with the reactor processor in one apparatus. 14. Installation according to claim 8, characterized in that the unit for heating hydrogen and / or hydrogen-containing media is combined in one apparatus with a reactor processor, and the heating of hydrogen and / or hydrogen-containing media is carried out due to the heat of the heated feedstock. 15. Installation for processing solid hydrocarbon raw materials, including preparation units, heating blocks for raw materials, blocks for producing final products, characterized in that the unit includes a block of finely divided solid hydrocarbons, the unit includes a unit for preheating molecular hydrogen and / or light hydrogen-containing media, enriched with hydrogen, for example, natural or associated gas, gas and light fractions of oil refining and petrochemicals, in particular gas and light fractions obtained in the process of According to this utility model, in addition to the installation, a reactor or reactor package with a catalyst heated to the required temperature to produce active atomic hydrogen and / or light radicals from molecular hydrogen and / or light hydrogen-containing media (unit for producing atomic hydrogen and / or light radicals), which are catalysts for the degradation of raw materials, the installation includes a processing reactor-processor in which hydrocarbon granules or powder of crushed raw materials are brought into direct interaction with the flow of atomic hydrogen and / or light radicals from a reactor with a catalyst (unit for producing atomic hydrogen and / or light radicals) to react with heated and / or cracked raw materials, the pressure in the unit for heating hydrogen and / or hydrogen-containing media and the reactor or the package of reactors with a catalyst is greater than the pressure in the processing reactor, light reaction products are continuously removed from the reaction zone and used in commercial product units to produce light commercial products a reactor-processor processing unit is combined with heating and / or cracking of raw materials in a single unit, and a reactor with a catalyst and a collector for the distribution of hydrogen atoms and / or radicals light over the cross section and volume of the processor reactor. 16. The installation according to clause 15, wherein the installation includes a unit for cleaning light reaction products from harmful impurities, as well as cooling and condensation units for the reaction products. 17. The apparatus of claim 15, wherein the apparatus includes a device for mixing particles (granules) of solid hydrocarbon feeds to prevent them from sticking together, and a reactor-processor of solid hydrocarbon feeds is combined with a mixing device. 18. The apparatus of Claim 15, wherein the apparatus includes purification and sorting units for partially reacted solid hydrocarbon feed, which is removed from the reaction zone, for returning the purified and sorted unreacted feed to the finely divided pulverizing unit or to the reaction zone to the reactor processor into which fresh solid hydrocarbon feed is introduced after the block of fine grinding. 19. The apparatus of Claim 15, wherein the apparatus includes a unit for purification of harmful impurities of unreacted hydrogen and / or light hydrogen-containing media enriched with hydrogen to return to the beginning of the process for reprocessing. 20. The apparatus of claim 15, wherein the unit for heating hydrogen and / or hydrogen-containing media and a catalyst is combined in one apparatus with a reactor processor, and the heating of hydrogen and / or hydrogen-containing media and a catalyst is carried out due to the heat of the heated feedstock.